Chromatography medium

ABSTRACT

The present invention provides a chromatography medium comprising one or more electrospun polymer nanofibres which in use form a stationary phase comprising a plurality of pores through which a mobile phase can permeate and use of the same.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a continuation of U.S. patent application Ser. No.16/422,102, filed May 24, 2019, which is a continuation of U.S. patentapplication Ser. No. 15/714,781, now U.S. Pat. No. 10,344,051, issuedApr. 5, 2018, which is a continuation of U.S. application Ser. No.14/356,817, now U.S. Pat. No. 9,802,979, issued Oct. 31, 2017, which isa national phase application under 35 U.S.C. § 371 that claims priorityto International Application No. PCT/GB2012/052768 filed Nov. 7, 2012,which claims priority to Great Britain Patent Application No. 1119192.1,filed Nov. 7, 2011, all of which are incorporated by reference herein intheir entirety.

FIELD OF INVENTION

The invention relates to chromatography medium, in particular to achromatography medium comprising one or more electrospun polymernanofibres which in use form a stationary phase comprising a pluralityof pores through which a mobile phase can permeate.

BACKGROUND TO THE INVENTION

The biotechnology market is the fastest growing sector within the worldpharmaceutical market accounting for 18% (S130 bn) of all market salesin 2010. This growth from 10% of the market share in 2002 is set to grow48% between 2010-2016 from 130 bn to 192 bn [1]. Biopharmaceuticaltherapeutics encompasses four main biomolecule types: recombinantproteins, monoclonal antibodies (MAbs), viral vaccines, and plasmid DNA[2]. There are currently over 200 MAb products on the market with over1000 in clinical trials [3]. As with most therapies there is a globalpressure to continue developing new biotherapuetics while driving downthe cost of production increasing their availability to a wider scope ofthe population [4,5]. This is particularly apparent to the downstreambioprocess (DSP) involved with the purification of biomolecules wherechromatography alone accounts for over 50% of the cost of goods (COGs).Advancements in upstream processes over the last 15 years have seenfermentation titres grow from 0.5 g/L-50 g/L, and with this not beingmimicked in the DSP there has been a clear drive in industry andacademia for development [6,7].

Conventional chromatography involves various techniques for theseparation of mixtures by passing a mobile phase through a stationaryphase. The analyte (load/feed) is the mobile phase which is passedthrough the solid stationary phase in the form of a packed bed systembased on adsorbent beads 50-100 μm in diameter. This stationary phasehas differing affinities for different species contained in the load.The species that are either wanted (product capture) or not wanted(contaminant capture) bind to the stationary phase allowing for thepurification of the product stream.

Affinity chromatography, developed by Pedro Cuatrecasas and Meir Wilchek[8], separates on the basis of a reversible interaction between abiomolecule and a specific ligand coupled to a chromatography matrix.The ligand most commonly used is Protein A due to its high selectivitywhich means equipment only needs to be scaled for product outputrequirements [9].

Other ligands in use include Protein G, Protein A/G and Protein L. Eachhas a different binding site recognizing different portions ofantibodies which becomes useful when the product are antibody fragmentsas opposed to a whole MAbs [10,11].

Ion exchange chromatography is a widely used technique for theseparation and purification of proteins, polypeptides, nucleic acids,due to its widespread applicability, high resolving power, high capacityand simplicity. Separation in ion exchange is obtained as biomoleculeshave ionisable chemical moieties which render them susceptible to chargeenhancement as a function of ionic strength and pH. This impliesbiomolecules have differing degrees of interaction with an ion exchanger(insoluble matrix to which charged groups have been covalently bound)due to differences in their charges, charge densities and distributionof charge on their surface.

At a pH value below its PI (isoelectric point) a protein (+ve surfacecharge) will adsorb to a cation exchanger (−ve). At a pH above its PI aprotein (−ve surface charge) will adsorb to an anion exchanger (+ve).

Consequently under a set of defined mobile phase conditions a biopolymermixture may be chromatographed using an ion-exchange medium in suitablecontactor. Dependent on the relative ionic charge of the components,some biopolymers will adsorb (adsorbates) and others will remain insolution. Desorption of bound material can then be effected resulting ina degree of purification of the target biomolecule [12].

The projected increase in the number of antibody therapies over the next4 years along with improvements in upstream productivity, and processeconomics gives a requirement for improved downstream processingtechniques. The limitations of chromatography systems are already beingseen in the form of expensive resins and throughput volumes which givesstrong argument to the demand for improving technologies in this field.

There are two major drawbacks of traditional packed bed columnchromatography; pressure drop and residence times. The operational flowrates in a packed column are limited by the pressure drop across thecolumn. The compressible packed bed is susceptible to high pressureswhich can have drastic consequences with implosion of the column itself.At such a stage in the bioprocess where material is extremely high valuethis can have severe economic impacts for any company. Packed bedcolumns usually employ porous ca. 50 μm diameter Agarose beads as highlyporous structures that achieve a suitable surface area for adsorption.However the system relies on diffusion for the large target biomoleculesto come into contact with these surfaces which requires long residencetimes. As such the flow rates must be kept at a relatively low value,often in the range of 100 cm/h, which therefore limits the throughput ofthe system. The concern here is regarding the inefficient use ofexpensive chromatography resins [13,14].

Membrane adsorbers have been commercially available for many years now,but these have only proven to be useful at small scale [15]. Usingmembrane chromatography allows for operation in convective mode therebysignificantly reducing the diffusion and pressure drop limitations seenin column chromatography. Operating at much higher flow rates offersadvantages such as decreasing process time thereby increasing throughputand reducing damage to product biomolecules due to shorter exposure tounfavourable medium [16].

Kalbfuss, et al. described how the use of a commercially available anionexchange membrane proved to be a potentially viable option for theremoval of viral particles operating in contaminant capture mode withrelatively high flow rates of 264 cm/h performing consistently well[21].

Zhou and Tressel carried out a cost analysis based on theirexperimentation using anion (Q) exchange membranes to remove four modelviruses. Results suggested that the economic viability of the Q membraneover the Q column was highly dependent of production scale along andspecific to each production process [22]. Research suggests that thereis potential for Q membranes though the advantages do not seemsignificant enough for the industry to adopt such a significant change.Additionally, chromatographic operations that run in capture mode suchas cation-exchange chromatography (CEX) and affinity chromatography haveproven to be much more challenging with poor peak resolution observed[23]. One aspect working in the favour of membrane chromatographysystems is the increased uptake of disposable systems in industry, ofwhich membranes hold many advantages over conventional packed bedcolumns.

There are many examples of membrane adsorbers in use and in continuingdevelopment [24-29].

It is clear from the work that is already published on membraneadsorbers that several important properties are required relatingspecifically to the membrane structure. For efficient utilisation ofbinding surface area the inlet flow must have even dispersion and thepore size distribution must be small so as to minimize any channelling.Membranes used in the chromatography method discussed above also excelwhen combined with other technologies.

Simulated Moving Bed (SMB) technology has been in use for many years inthe chemical industry, originally developed for difficult petrochemicalseparations [32]. Later its use in the pharmaceutical industry quicklygrew due to its strong ability to perform chiral separations with thefirst US Food and Drug Administration's (FDA) approved drug manufacturedby SMB technology reaching the market in 2002 with Lexapro [33].Traditionally the powers of SMB to carry out separation based on thedifferent moieties of complex components have been focused on systemsthat yielded poor productivity using column chromatography. Todayhowever more focus is being placed on bind/elute chromatographicprocesses in an effort to improve the utilisation of expensiveadsorptive resins and reduce the large volumes of buffers used at largescale production [34,35].

In this fashion SMB chromatography operates by employing three or morefixed adsorbent substrates, such as packed bed columns, with buffer andfeed streams flowing into to system continuously. A counter-currentsolid substrate is simulated by switching various valve inlet portsperiodically.

SUMMARY OF THE INVENTION

A first embodiment of the invention relates to a chromatography mediumcomprising one or more electrospun polymer nanofibres which in use forma stationary phase comprising a plurality of pores through which amobile phase can permeate. The invention may also be a chromatographymedium having a plurality of pores comprising one or more polymernanofibres. Typically, the stationary phase is a membrane of nanofibres,which may have a thickness of 10 nm to 15 mm, often 10 μm-10 mm, or 100μm-1 mm Ensuring that the membranes do not exceed these parameters isdesirable as, if a membrane is too thin, the membrane may rupture underhigh flow rates and if a membrane is too thick, blockages may occurwhich could lead to damaging build ups of pressure and/or decreasedperformance.

The polymer nanofibres may be non-woven nanofibres. Using a randomlydeposited fibre mat (non-woven) structure can encourage impeded flowthereby discouraging channelling [30].

The polymer nanofibres are electrospun. Electrospinning providesnanofibres with consistent dimensions and can easily be tuned (forexample, by varying atmospheric properties while spinning) to makenanofibres of different proportions. Electrospinning is a technique thatalso demonstrates excellent distribution properties, especially usefulwhen creating layered membranes [31]. Nanofiber mass transfercharacteristics have been shown to be similar to those in a monolithstructure which allow for flow rate independent separations [43].

The polymer used in the present invention is not limited to any specificpolymer and can be tailored for specific use. The polymer may be forexample: nylon, poly(acrylic acid), polyacrylonitrile, polystyrene,polysulphone, polyacrylonitrile, polycaprolactone, collagen, chitosan,agarose and polyethylene oxide and and combinations thereof. The polymermay be derivatised to enhance the solubility and/or other properties ofthe polymer in order to improve its suitability to be electrospun. Thederivatised polymer (for instance polyether sulfone, cellulose acetateor poly(acrylonitrile-co-acrylic acid) can be treated postelectrospinning to regenerate the original polymer or derivatise furtherto create a new functionality. The polymer used in the invention istypically cellulose. Cellulose is often used as it is readily available,cheap, biodegradable, biologically compatible and has a hydrophilicsurface resulting in low non-specific binding.

The polymer nanofibres may be covalently cross-linked. Once anelectrospun network of nanofibres has been made, the nanofibres may befused together at points were nanofibres intersect one another bythermal, chemical or other methods. This leads to improved manualmanipulation characteristics.

The nanofibres may have a diameter of 10 nm to 1000 nm. The nanofibresmay have a diameter of 200 nm to 800 nm and may even have a diameter of300 nm to 400 nm. Nanofibres of this size yield improved consistency ofpore size and size distribution.

The nanofibres may have a mean length of greater then 10 cm. Nanofibresgenerated by electrospinning are typically much longer than thenanofibres found in conventional chromatography media. Longer nanofibresdeliver improved layering properties. In some cases, where theelectrospinning comprises a fibre emanating from a single source, asingle continuous fibre may be produced and the membrane formed fromthis fibre alone, or from a small number (1, 2, 3, 4, 5, 6, 7, 8, 9, 10)of long fibres.

The pores of the stationary phase may be 10 nm to 10 μm in diameter,often 25 nm to 5 μm and can be 50 nm to 2 μm in diameter. Use of poresizes within these size ranges can help to minimise fouling of thechromatography medium and decrease product loss due to polarization,concentration and rejection at particle interfaces [18]. However, thepores remain small enough to minimise the loss of target componentspassing through the membrane without coming into contact with themedium. The selection of these pore sizes ensures good utilisation ofcapacity [19] and sharper breakthrough curves [20]. Kaur et al. [39]demonstrated that for a membrane structures with similar pore size thenanofibre structures were 1.5-2 times more permeable to aqueous flowthan a traditional membranes produced by phase inversion. This is due tothe relatively high surface porosity that the electrospinning processyields. Ziabari et al. [40] showed that a non-woven nanofibre membranewith average fibre diameter of 300 nm contained an average pore size ofca. 500 nm, yet yielding a porosity of 49%. By electrospinning nanofibremembranes we are able to achieve a high level of surface porosity ofhigh distribution well above what could be expected from traditionallyformed membranes as in their case the relationship of decreasing surfaceporosity with decreasing pore size is dominant [41].

The pores may have a narrow size distribution, wherein the standarddeviation in pore diameter is preferably less than or equal to 250 nm.Pore size uniformity is one of several factors as well as, axial andradial diffusion and sorption kinetics, that has been shown to have animpact on key performance factors in chromatography (particularlyaffinity chromatography) such as breakthrough curve (BTC) sharpness[17].

A second embodiment of the invention relates to the use of the media inchromatography. The medium is typically for use in ion exchangechromatography and may also be for use in affinity capturechromatography. Ion exchange and affinity capture chromatography areparticularly suitable for use with the chromatography medium of theinvention as the medium can be readily functionalised to interact withtarget molecules. This gives the medium high capacity whilst allowinglarge volumes to be processed. Multi-point attachment of ligands and thelike to the medium is possible and gives minimal leakage and results inlow product contamination.

The invention may also be for use in isolating biological molecules fromthe mobile phase. Typically, these biological molecules have a molecularweight of 1 kDa to 200 kDa and may have a molecular weight of 10 kDa to100 kDa. Often monoclonal antibodies are of molecular weight around 150kDa, often in the range 100-200 kDa. The invention may be used toisolate biological molecules selected from: recombinant proteins,monoclonal antibodies, viral vaccines and plasmid DNA.

The invention may also be for use in enzyme catalysed reactions.Typically enzymes are immobilised on the nanofibres. The enzymes may beimmobilised by adsorption, entrapment or cross-linkage.

The invention also typically employs a simulated moving bed (SMB)system. The SMB system can be employed so as to exploit the fast masstransfer properties of the nanofibre adsorbents. This leads to a greaterutilisation of the medium performing the desired separation of the feedstream yielding a continuous product stream by switching outlet ports[36-38]. Further, SMB chromatography lends itself well for industrial,continuous purification as does the medium of the invention which may bea membrane. Membranes are easier to replace than conventionalchromatography media (e.g. silica powder) and therefore leads to reduceddisruption of continuous purification processes.

In embodiments of the invention employing an SMB system flowdistribution may be optimised for maximum utilisation of the adsorbent.Preferably the fluid is in plug flow. Plug flow allows mass transferacross the entire binding surface of the adsorbent and can provideimproved separation, as measured for example by BTC sharpness.

A third embodiment of the invention relates to a cartridge for use inchromatography comprising: two or more membranes including the medium ofthe invention arranged in series; and a holding member to fix themembranes in place relative to one another. Including multiple membranesfurther improves the cartridge's filtration performance. Providing themedium in the form of a cartridge also allows the medium be easilyinserted and removed from industrial purification systems. The holdingmembers support the nanofibre membrane and aid flow distribution.

In some examples the membranes may be interspersed with frits. As usedherein the term “frit” is intended to be given it's common meaning inthe art, and refers, for instance, to a rigid porous structure. Thefrits may offer support and promote dispersion in an effort to createplug flow to maximise utilisation of the adsorbent surface. The ratio ofmembranes to frits may be in the range 5:1-1:5. Interspersion may beregular, wherein a regular pattern of membrane to frit is provided, suchas membrane-membrane-frit in a 2:1 membrane:frit system, or irregular,wherein the ratio of membrane:frit is as defined, but the ordering ofthe layers does not form a pattern. In many cases, there will be moremembranes than frits, and so the ratio of membranes:frits would be inthe range 5:1-1:1. Often the ratio of membranes:frits will be 1:1, andthe interspersion will be a regular membrane-frit-membrane-frit pattern.

DESCRIPTION

The invention will now described by reference to the following figures:

FIG. 1 shows a schematic image of the cartridge of the invention;

FIG. 2 shows an alternative embodiment of the cartridge of theinvention; and

FIG. 3 shows an exploded image of the embodiment of FIG. 2.

FIG. 4a shows binding/elute profiles of a nanofibre cartridge of theinvention at varying flow rates in which, starting from light grey fullline to dark grey dotted line: 72 cm/h (2,400 CV/h), 96 cm/h (3,200CV/h), 120 cm/h (4,000 CV/h), 240 cm/h (8,000 CV/h) and 360 cm/h (12,000CV/h). FIG. 4b shows a chromatogram showing 10 repeat bind/eluteprofiles of a nanofibre cartridge of the invention at a fixed loadingflow rate of 240 cm/h (8,000 CV/h).

FIG. 5 shows SEM images of a nanofibre cartridge of the invention andSartobind IEXD membrane before and after a feed stream of centrifugedand 0.45 μm filtered yeast homogenate. Top SEM images show cleanmembranes at two magnifications, while the bottom images show membranesafter 50 cycles of clarified homogenate loading. The scale bar indicates10 μm.

FIG. 6a shows the results of a filtered load investigation showingpressure flow relationships for equivalent volumes of: 0 Sartobind IEXD,0 Sartobind Epoxy-DEAE, and ⋄ DEAE nanofibre of the invention. Errorbars are ±1 standard deviation of the sample population. FIG. 6b showstwo bind/elute profiles before and two after clarified homogenateloading and CIP of the DEAE nanofibre cartridge of the invention at afixed loading flow rate of 240 cm/h to demonstrate reproducibility afterclarified yeast homogenate loading (2 mL) and CIP (20 mL 1M NaOH).

FIG. 7 shows a design drawing of a simulated moving bed (SMB) systemshowing different phases of operation.

FIG. 8 shows the average separation results for DEAE nanofibre adsorbentof the invention (Black) and Sartobind IEXD (Dark Grey). ±1 standarddeviation of the sample population is shown by the shaded grey areaaround each curve.

FIG. 9 shows an SDS Page Gel showing denatured components of 12 proteinsamples.

FIG. 10 shows chromatogram data from the SMB operation of 2-componentseparation; UV absorbance traces were a snapshot for a 25 second timeperiod taken from the three different adsorbent columns during one SMBoperation.

FIG. 11 shows photographs from a coomassie blue dye flow distributionstudy utilising different pore size frits.

As shown in FIG. 1, cartridge (1) comprises a holding member (2) withinwhich multiple membranes (3) are arranged in series. In this embodiment,one or more frits (6) are also present, in a 1:1 ratio with themembranes of the invention. The cartridge also has an inflow port (4)through which a mobile phase can be passed and a corresponding outflowport (5).

FIGS. 2 and 3 show an alternative embodiment of the cartridge of theinvention. In this embodiment holding member (2) comprises a supportcolumn (7) onto which the membranes (3) and, where present, frits (7),may be placed.

Unless otherwise stated each of the integers described in the inventionmay be used in combination with any other integer as would be understoodby the person skilled in the art. Further, where numerical ranges areprovided, it is intended that these represent a specific disclosure notonly of the end points of the range, but of each value, in particularintegers, within the range. In addition, although all aspects of theinvention preferably “comprise” the features described in relation tothat aspect, it is specifically envisaged that they may “consist” or“consist essentially” of those features outlined in the claims.

EXAMPLES

A solution of cellulose acetate (CA) (Mr=29,000; 40% acetyl groups; 0.20g/mL) in acetone/dimethylformamide/ethanol (2:2:1) was electrospun toobtain CA nanofibre non-woven membranes.

Sartorious Stedim Sartobind membranes (Sartorius Stedim UK Ltd. Epsom,UK) were cut to size and used as a comparison.

Electrospinning

The process was carried out in a ClimateZone climate control cabinet(a1-safetech Luton, UK) which allows the process to be performed undercontrolled atmospheric conditions. The temperature and RH were selectedand kept constant throughout the fabrication at 25° C. and 60% RH.

A 50 mL polymer solution was loaded into a sterile syringe and attach toa Harvard PHD 4400 syringe pump (Harvard Apparatus Ltd. Kent, UK), witha programmable flow rate range from 0.0001 up to 13.25 L/h, to deliverthe polymer solution to a 0.5-mm ID stainless steel micro needle. Thepump is set at a flowrate of 800 μL/h. The tip of the needle was placed30 cm above the grounded collector. The collector used was an earthedaluminium rotating drum (15 cm diameter×25 cm width) covered with lowsurface friction polymer rotating at a speed of 100 rpm. The process wasrun for 60 h. These conditions were selected based on preliminaryexperiments and are known to yield solid dry nanofibres with diametersfrom 300-400 μm.

Post Electrospinning Modification

Once electrospun the nanofibres are removed from the collection drum andplaced into a drying oven at 213° C. for ten minutes. This is below theglass transition temperature of cellulose acetate but it is hot enoughto begin fusing joints where nanofibres intersect, thereby increasingthe structural stability of the fibre matt giving improved manualmanipulation characteristics.

After this process the fibre matt is cut into multiple 25 mm diameterdiscs using a wad punch. These discs are then ready for packing into aPALL Easy Pressure Syringe Filter Holder (Pall Life Sciences,Portsmouth, United Kingdom).

Once packed into a ˜100 mg cartridge (˜6 layers ˜0.4 mm bed height) themembrane is treated with 200 mL 0.1M NaOH in a solvent mixture of 2:1De-ionised (DI) H₂O:Ethanol for 24 hours fed continuously in a cyclicalmanner using a Watson Marlow 205U Peristaltic pump (Watson-Marlow PumpsGroup Falmouth, UK) at a rate of 15 mL/min. After thesaponification/deacetylation process to form a regenerated cellulosemembrane 200 mL DI H₂O is passed through the membrane at the sameflowrate. Anion-exchange surface functionality is then obtained byrecycling 20 mL warm (40° C.) 15% DEACH aqueous solution at 20 mL/minfor 10 minutes. Cartridges are subsequently removed from the filterholder housing and left in 20 mL hot (80° C.) 0.5M NaOH on a hot platestirrer with gentle agitation. Finally the membrane cartridges arerinsed in multiple volumes of DI H₂O before being packed ready for use.

Permeability

The permeabilities of load and buffer solutions through packed nanofibrewere compared with the permeabilities of a commercially availablealternative membrane, Sartorious Sartobind membrane, using an AKTAExplorer (GE Healthcare Life Sciences, Buckinghamshire, UK) with onlinepressure measurement capabilities. The pressure drop of the system wasfirst evaluated using the empty membrane holder evaluated at flow ratesranging from 1 mL/min-100 mL/min. The different membranes were thenevaluated with the system pressure drop being subtracted to calculatethe permeability of each membrane at the varying flow rates.

Equilibrium Binding

The previously prepared 25 mm diameter AEX membrane cartridges have atotal film surface area of 4.91 cm², an approximate mass of 100 mg, andan approximate wet bed height of 0.3 mm suggesting a bed volume ˜0.17mL. Equilibrium binding studies were carried out to find the totalcapacity of the DEAE AEX membranes for of a model protein Bovine SerumAlbumin (BSA). This was carried out in the sealed filter holder systemusing sterile disposable syringes (BD biosciences) and a Harvard PHD4400 syringe pump (Harvard Apparatus Ltd. Kent, UK). The DEAE membranewas equilibrated with 10 mL wash buffer 10 mM Tris, pH 8.0 buffer a rateof 40 mL/min 20 mL of lmg/mL BSA (in wash buffer) was then loaded ontothe membrane at a rate of 40 mL/min. This load sample was then pulledback through the membrane at the same rate with this process beingrepeated continuously for 1 hour in order to expose the membrane to themodel protein for a sufficient length of time to reach maximum bindingcapacity. Collection of the load stage was followed by five wash stageswith 1 mL wash buffer before desorption of the model protein was carriedout by three elution stages each with 1 mL 1M NaCl 10 mM Tris, pH 8.0elution buffer at a rate of 40 mL/min.

All wash and elution stages followed the same dual flow pattern usedwith the loading for a period of two minutes each. At each stage in thisprocess the eluate was collected and UV absorbance readings at 280 nmwere taken using Jasco V-630 UV spectrophotometer (Jasco (UK), Essex,United Kingdom). Studies were repeated on three occasions in order toensure replicates were reproducible. Mass balances were conducted toensure the traceability of all model protein introduced into the system.The same protocol was run with Sartobind DEAE membranes and Sartobindepoxy membrane functionalised in house for comparison. Control sampleswere run under the same conditions to discount possible binding to thefilter holder surface or non-specific binding of BSA tonon-functionalised membrane, regenerated cellulose (RC) membrane.

Dynamic Breakthrough

A more useful determination of the binding capacity of these nanofibreadsorbents is their dynamic binding capacity employing operationalflowrates observed as suitable in previous permeability studies.Experiments were completed using the AKTA Explorer (GE Healthcare LifeSciences, Buckinghamshire, UK) with online measurement of UV absorbance(280 nm), pH, and conductivity.

DEAE nanofibre membrane cartridges were prepared in the same way asbefore in order to determine the dynamic capacity of the membranes forof a model protein Bovine Serum Albumin (BSA). The DEAE membrane wasequilibrated with 10 mL wash buffer 10 mM Tris, pH 8.0 buffer a rate of6000 CV/h. 1 mg/mL load sample of BSA were then loaded onto the membraneuntil 100% breakthrough at various flow rates from 24,000 CV/h-4000CV/h. 10 mL wash buffer was then passed through the saturated membranebefore 5 mL 100% 1M NaCl 10 mM Tris, pH 8.0 elution buffer wasintroduced to the membrane at a range of flow rates from 8000 CV/h-2000CV/h.

Online UV absorbance readings at 280 nm were taken throughout theexperiment.

A simulated moving bed system was designed and built using a series ofBurkert solenoid valves (Bürkert Fluid Control Systems, Stroud, UK)1/16″ Peek tubing, Peek connectors, and a Perimax 12 peristaltic pump(Spetec GmbH, Erding, Germany). UV sensors were placed on the exit ofeach of the three filter holders which was connected to a NationalInstruments analogue input module (National Instruments Corporation(U.K.) Ltd, Newbury, UK) to record the UV absorbance at 280 nm. ThreeNational Instrument digital output modules were used to control thevalve positions with NI Labview 2010 software used to sequence thecontrol and compute the analogue input signals.

Chemical Surface Derivatisation (FT-IR)

ATR-FTIR spectrum of the CA, RC and modified RC membrane was obtained ona Thermo Scientific Nicolet iS10 FT-IR Spectrometer fitted with anattenuated total reflectance (ATR) module (Loughborough, UK) TheAttenuated total reflectance technology allows for direct analysis ofsolid, liquid or gas samples without further preparation. Spectra wererecorded in the range 4000-500 cm⁻¹ by an accumulation of 50 scans. Abackground was measured with 10 scans prior to each sampling. Themanufacturer supplied software OMNIC was used to normalise and analysethe spectra.

Scanning Electron Microscopy (SEM)

A Hitachi TM-1000 Tabletop microscope (Hitachi High-Technologies EuropeGmbh) was used to monitor the physical properties of the nanofibresafter electrospinning and during/post modification to ensure than thenanofibre form remained consistent. Samples were analysed from three SEMimages each with 20 individual measurements of nanofibre diameters.

Protein Concentration (UV)

UV spectrophotometer Jasco V-630 (Jasco (UK), Essex, United Kingdom) wasused to determine the concentration of BSA in solution. A full spectrumfrom 320 nm-240 nm was recorded with a scan speed of 200 nm/min and astep of 1 nm.

AKTA Explorer (GE Healthcare Life Sciences, Buckinghamshire, UK) wasused to measure online absorbance at 280 nm, pressure, feed rates andconductivity throughout the experiments allowing for full run profilesto be analysed.

Reproducibility, Mass Transfer, and Life Cycle Performance

Reproducibility in performance was shown based upon 10 bind/elute runsof the DEAE nanofiber cartridge at a fixed loading flow rate of 240cm/h. The absorbance flow profiles shown in FIG. 4b clearly show thatthe adsorbent operates in a reproducible manner during laboratory scaleexperiments using standard liquid chromatography apparatus.

Bind/elute profile of the DEAE nanofibre cartridge at varying flow rateswas also investigated and is shown in FIG. 4a : starting from light greyfull line to dark grey dotted line; 72 cm/h (2,400 CV/h), 96 cm/h (3,200CV/h), 120 cm/h (4,000 CV/h), 240 cm/h (8,000 CV/h) and 360 cm/h (12,000CV/h). The nanofibre adsorbents demonstrated high mass transfercharacteristics that are desired for a high productivity separation withno observed peak broadening in the separation with increased flow ratewhen plotting the chromatogram against time indicating that masstransfer is a minimal component of the resistance in the column. Theintegrated areas of the elution peaks in the UV absorbance profilesremained constant demonstrating equivalent capture and elution over therange of flow rates tested. The adsorbents tested had a bed height of0.3 mm and column volume of ˜0.15 mL.

Fouling studies utilized clarified yeast homogenate to give anunderstanding of how the adsorbent would perform with complex loadconditions. Initial adsorbent fouling studies conducted in aconventional process manner showed no change in trans-bed pressure over50 cycles of loading, washing, eluting, cleaning-in-place (CIP), andequilibration. Scanning electron microscopy images showed no visiblebuild-up of homogenate on the nanofibre adsorbents after 50 cycles.Conversely, the Sartobind IEXD membranes showed some fouling (FIG. 5)illustrating that with standard CIP conditions (1M NaOH) nanofibreadsorbents were more easily cleaned.

In the continuous homogenate loading experiments both the DEAE nanofibrecartridge and Sartobind IEXD membrane performed well with the clarifiedhomogenate; running for over 9,000 column volumes with only a smallincrease in trans-bed pressure (FIG. 6a ). The Sartobind Epoxy-DEAEderivatized membrane was affected more by this homogenate most likelydue to the smaller pore sizes in this membrane. The chromatogram of BSAcapture by nanofibre adsorbent before and after clarified homogenateloading and CIP shown in FIG. 6b demonstrates that the nanofibrecartridge performed reproducibly irrespective of the complex feed andharsh CIP conditions employed, confirming the observation shown in FIG.5 that there was little build-up of homogenate on the nanofibre surfaceduring these studies.

Simulated Moving Bed Operation

A simulated moving bed (SMB) system was designed and built using aseries of Burkert solenoid valves (Bürkert Fluid Control Systems,Stroud, UK), 1/16″ Peek tubing, Peek connectors, and three Dionex P580 PHPLC pumps (Dionex Softron GmbH, Germany). UV sensors were placed on theexit of each of the three adsorbent holders which were connected to aNational Instruments analogue input module (National InstrumentsCorporation (U.K.) Ltd, Newbury, UK) to record the UV absorbance at 280nm. Three National Instrument digital output modules were used tocontrol the valve positions with NI Labview 2010 software used tosequence the control and compute the analogue input signals. FIG. 7shows the SMB design layout operating at 3 different phases of theprocess.

Use of Nanofibre Adsorbents in the SMB System

The mass transfer properties of these nanofibre adsorbents make themideally suited to SMB operation where product can be rapidly loaded andremoved in a multiple reuse fashion. FIG. 8 shows the flow through ofcytochrome C+ unbound BSA as the first peak during loading of2-component mixture and the elution of BSA as the second peak. Thegraphs show the reproducibility over 12 equivalent runs for eachadsorbent type. This shows that for the conditions chosen, the nanofibreadsorbents performed favourably for an equivalent volume of adsorbent.The nanofibre adsorbent captured and eluted 99% of the BSA loaded,whereas the Sartobind IEXD membrane only captured 70%. Over the 12 runsfor each adsorbent the standard deviation was calculated to show thatthe nanofibre adsorbent operated more consistently, though both typesdemonstrated high levels of consistency. The results shown in FIG. 8demonstrate that for the conditions chosen the nanofibre adsorbentcaptured and eluted more of the target molecule (BSA) from the2-component mixture. The tighter shaded region also indicates a moreconsistent performance in separation. In each case the adsorbent testedhad a bed height of 0.3 mm and column volume of ˜0.15 mL

Samples from the 2-component separation studies were separated by SDSPage for analysis and the gel shown in FIG. 9 confirms the results shownin FIG. 8. The samples run in the gel included samples from both ATKAand SMB studies, and from both nanofibre IEXD and sartobind IEXDadsorbents. The Sartobind IEXD membranes did not capture all of the BSAduring the loading, which is expressed by the 66 kDa band that can beseen in the flow through sample (well 6) on the gel. In contrast theflow through sample from the nanofibre adsorbent (well 4) indicates noBSA present. The same is observed in wells 9 and 10 showing the flowthrough from 2 Nanofibre DEAE SMB runs. Wells 7 and 8 show the productstreams from 2 Nanofibre DEAE SMB runs which indicated the same resultas the product stream of the separation carried out on the AKTA Basic(well 3), where BSA was present in the eluate but Cytochrome C was not.Wells 11 and 12 show the components of the product and waste streamsduring an SMB run using Sartobind IEXD membranes. The product streamcontained only BSA but the waste stream appeared to contain bothCytochrome C and BSA suggesting that not all the BSA was being capturedas seen with the AKTA Basic separation in well 6. The gel indicates thatthe nanofibre adsorbents performed preferentially in both the modes ofoperation.

Throughput and Productivity

The SMB system relies on a series of valves to switch at given timepoints to direct the flow of the different mobile phases. In order tooptimise the performance of the system, and therefore productivity, the18 valves must direct the different phases to different locations atexactly the right time. Once optimisation of productivity for the2-component system was complete 200 mg BSA was repeatedly purified fromthe two-component protein mixture in 7.5 minutes using three columnvolumes of 0.15 mL implying an overall system productivity of 1.72g/hour. This relates to a system productivity of 3.92 g (product)/mL(adsorbent)/hour.

Dynamic Binding Operating Capacity Flowrate Productivity Adsorbent(mg/mL) (CV/h) (cm/h) (g/mL/h) Nano-DEAE 10 12000 360 3.92 Sarto-IEXD6.5 6000 180 1.22 DEAE Sepharose 110 24 60 0.1

Table 1 shows data comparing the average productivities of the DEAEnanofibre adsorbents and the Sanobind IEXD achieved during SMBoperation. Operational flow rates were chosen to maintain a standardpressure drop of 0.125 bar across the different adsorbents. Productivitycalculations (expressed as Grams of product per Millilitre of adsorbentper Hour) were based on the following column dimensions: Porous beadedsystem 0.7×2.5 cm (W×H). other adsorbents 2.5×0.204 cm (W×H).

Data collected by the three SMB UV sensors is shown in the chromatogramof FIG. 10. The signal created by the sensors was fed back into the NIanalogue input module and recorded by a Labview program that wasspecifically written for this purpose. The traces show how all threeadsorbent columns operated similarly and how the different phases ranthrough each column at a particular time. The flow through was observedas the smaller peak containing Cytochrome C and the larger elution peakcontaining the target molecule, BSA. The high level of consistencyobserved highlights the suitability of these nanofibre adsorbents foroperation in continuous processing applications.

The productivity that was achieved was limited by the simple design ofthe SMB system which utilised only three adsorbent modules in sequenceand could only be run at 360 cm/h due to the limitations of the SMBsystem. Productivity calculations were based on chromatography cycletimes for the loading, washing, elution, and regeneration of theadsorbents for set flow rates. Using the productivity ratios that wereestablished at the SMB system's limits productivities for higher flowrates were extrapolated based on the known pressure drop limitations ofeach type of adsorbent. In a previous study it was shown that thenanofiber adsorbents could operate at a flowrate of 2,400 cm/h with apressure drop across the adsorbent of less than 0.5 bar [31]. For theDEAE Sepharose comparison phase lengths were taken from recommendedvalues in literature [42].

Dynamic Binding Operating Calculated Capacity Flowrate ProductivityAdsorbent (mg/mL) (CV/h) (cm/h) (g/mL/h) Nano-DEAE 10 (±0.3)  800002,400 26 Sarto-IEXD 6.5 (±0.71) 40000 1,200 5 DEAE Sepharose 110 150 3750.6

Table 2 shows data comparing the potential productivity of theadsorbents operating at their maximum established flow rate for apressure drop of 0.5 bar. Productivity calculations (expressed as Gramsof product per Millilitre of adsorbent per Hour) were based on thefollowing column dimensions: Porous beaded system 0.7×2.5 cm (W×H),other adsorbents 2.5×0.204 cm (W×H).

Flow Distribution

To facilitate suitable flow distribution of media through theseadsorbent materials a bespoke adsorbent holder was machined. In additionto this suitable packing of the adsorbent into bespoke adsorbent holdersis required to promote flow distribution. To evaluate flow distribution,a dye solution (Coomassie Brilliant Blue dissolved in 20 mM Bis-Trisbuffer, pH 5.8) was loaded onto the adsorbent.

After loading with a dye solution the adsorbent holder was disassembledto show the suitable coverage of the flow showing even flowdistribution. FIG. 11 shows the photographs of the adsorbents after thedye flow distribution study which utilised 3 different stainless steelfrits containing different pore sizes. The formation of air bubblesunderneath the frit also presented an issue for flow distribution butthese would be removed by flowing 20% ethanol through the packed bedprior to normal operation.

The photographs from the flow distribution study shown in FIG. 11demonstrate the requirement for creating distribution prior to loadingonto these adsorbents. A 5 μm stainless steel frit offered the most evendistribution that would be required to utilise the adsorbents to theirmaximum efficiency. The removal of air bubbles underneath the frit isalso required by the flow through of 20% ethanol prior to normaloperation.

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We claim:
 1. A chromatography medium comprising a non-woven fabriccomprising one or more polymer nanofibres wherein the polymer nanofibersare fused together at points where the nanofibers intersect one another,and which form a stationary phase comprising a plurality of poresthrough which a mobile phase can permeate, and wherein thechromatography medium has affinity chromatography protein ligand surfacefunctionality interactive with target molecules.
 2. The medium accordingto claim 1, wherein the stationary phase is in the form of a membrane.3. The medium according to claim 1, wherein the affinity chromatographyprotein ligand surface functionality comprises a Protein A ligand,Protein G ligand, Protein A/G ligand, or Protein L ligand.
 4. The mediumaccording to claim 3, wherein the affinity chromatography protein ligandsurface functionality comprises a Protein A ligand.
 5. The mediumaccording to claim 2, wherein the membrane has a thickness of 100 μm to1 mm.
 6. The medium according to claim 1, wherein the polymer isselected from: nylon, poly(acrylic acid), polyacrylonitrile, polystyreneand polyethylene oxide.
 7. The medium according to claim 1, wherein thepolymer is cellulose.
 8. The medium according to claim 1, wherein thepolymer nanofibres are covalently cross-linked.
 9. The medium accordingto claim 1, wherein the nanofibres have a diameter of 10 nm to 1000 nm.10. The medium according to claim 1, wherein the nanofibres have adiameter of 200 nm to 800 nm.
 11. The medium according to claim 1,wherein the nanofibres have a diameter of 300 nm to 400 nm.
 12. Themedium according to claim 1, wherein the mean length of nanofibres isgreater than 10 cm.
 13. The medium according to claim 1, wherein thepores have a diameter of 10 nm to 10 μm.
 14. A chromatography methodusing the medium according to claim
 1. 15. The method according to claim14, wherein the chromatography is affinity capture chromatography. 16.The method according to claim 14, wherein the medium is used to isolatebiological molecules from the mobile phase.
 17. The method according toclaim 16, wherein the biological molecules have a molecular weight of 1kDa to 200 kDa.
 18. The method according to claim 14, wherein thebiological molecules are selected from the group comprising: recombinantproteins, monoclonal antibodies, viral vaccines and plasmid DNA.
 19. Themethod according to claim 14, wherein a simulated moving bed system isemployed.
 20. A cartridge for use in chromatography comprising: two ormore membranes including the medium according to claim 2 arranged inseries; and a holding member to fix the membranes in place relative toone another.